CN108144555A - A kind of fluidized bed reactor - Google Patents
A kind of fluidized bed reactor Download PDFInfo
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- CN108144555A CN108144555A CN201810107889.1A CN201810107889A CN108144555A CN 108144555 A CN108144555 A CN 108144555A CN 201810107889 A CN201810107889 A CN 201810107889A CN 108144555 A CN108144555 A CN 108144555A
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- 239000003054 catalyst Substances 0.000 claims abstract description 41
- 239000000463 material Substances 0.000 claims abstract description 21
- 230000008602 contraction Effects 0.000 claims description 22
- 239000007788 liquid Substances 0.000 claims description 15
- 230000002093 peripheral effect Effects 0.000 claims 1
- 239000012071 phase Substances 0.000 abstract description 48
- 230000000694 effects Effects 0.000 abstract description 25
- 238000000926 separation method Methods 0.000 abstract description 14
- 239000007791 liquid phase Substances 0.000 abstract description 11
- 238000005984 hydrogenation reaction Methods 0.000 abstract description 10
- 238000005516 engineering process Methods 0.000 abstract description 4
- 238000006243 chemical reaction Methods 0.000 description 19
- 239000007789 gas Substances 0.000 description 18
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 description 7
- 239000001257 hydrogen Substances 0.000 description 7
- 229910052739 hydrogen Inorganic materials 0.000 description 7
- 238000009835 boiling Methods 0.000 description 6
- 239000007787 solid Substances 0.000 description 5
- 239000000470 constituent Substances 0.000 description 4
- 238000000034 method Methods 0.000 description 4
- PNEYBMLMFCGWSK-UHFFFAOYSA-N Alumina Chemical compound [O-2].[O-2].[O-2].[Al+3].[Al+3] PNEYBMLMFCGWSK-UHFFFAOYSA-N 0.000 description 3
- 230000001154 acute effect Effects 0.000 description 3
- 230000003197 catalytic effect Effects 0.000 description 3
- 230000007812 deficiency Effects 0.000 description 3
- 238000002474 experimental method Methods 0.000 description 3
- 239000012530 fluid Substances 0.000 description 3
- 239000007792 gaseous phase Substances 0.000 description 3
- 239000011344 liquid material Substances 0.000 description 3
- 238000004062 sedimentation Methods 0.000 description 3
- 239000011949 solid catalyst Substances 0.000 description 3
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 2
- 239000010426 asphalt Substances 0.000 description 2
- 239000003795 chemical substances by application Substances 0.000 description 2
- 235000013399 edible fruits Nutrition 0.000 description 2
- 239000012263 liquid product Substances 0.000 description 2
- 238000011068 loading method Methods 0.000 description 2
- 239000002245 particle Substances 0.000 description 2
- 239000002994 raw material Substances 0.000 description 2
- 239000007790 solid phase Substances 0.000 description 2
- 230000003321 amplification Effects 0.000 description 1
- 238000006555 catalytic reaction Methods 0.000 description 1
- 239000003245 coal Substances 0.000 description 1
- 239000011280 coal tar Substances 0.000 description 1
- 238000004939 coking Methods 0.000 description 1
- 230000000052 comparative effect Effects 0.000 description 1
- 230000006837 decompression Effects 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 238000000605 extraction Methods 0.000 description 1
- 238000011049 filling Methods 0.000 description 1
- 239000003350 kerosene Substances 0.000 description 1
- 229910052751 metal Inorganic materials 0.000 description 1
- 239000002184 metal Substances 0.000 description 1
- 239000004005 microsphere Substances 0.000 description 1
- 238000002156 mixing Methods 0.000 description 1
- 239000000203 mixture Substances 0.000 description 1
- 229910052750 molybdenum Inorganic materials 0.000 description 1
- 229910052759 nickel Inorganic materials 0.000 description 1
- 229910052757 nitrogen Inorganic materials 0.000 description 1
- 238000003199 nucleic acid amplification method Methods 0.000 description 1
- 239000003027 oil sand Substances 0.000 description 1
- TWNQGVIAIRXVLR-UHFFFAOYSA-N oxo(oxoalumanyloxy)alumane Chemical compound O=[Al]O[Al]=O TWNQGVIAIRXVLR-UHFFFAOYSA-N 0.000 description 1
- 238000000819 phase cycle Methods 0.000 description 1
- 238000005191 phase separation Methods 0.000 description 1
- 238000010992 reflux Methods 0.000 description 1
- 239000003079 shale oil Substances 0.000 description 1
- 230000003068 static effect Effects 0.000 description 1
- 229910052721 tungsten Inorganic materials 0.000 description 1
Classifications
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
- B01J8/18—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles
- B01J8/24—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles according to "fluidised-bed" technique
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
- B01J8/18—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles
- B01J8/1845—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles with particles moving upwards while fluidised
- B01J8/1854—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles with particles moving upwards while fluidised followed by a downward movement inside the reactor to form a loop
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
- B01J8/18—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles
- B01J8/1872—Details of the fluidised bed reactor
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G49/00—Treatment of hydrocarbon oils, in the presence of hydrogen or hydrogen-generating compounds, not provided for in a single one of groups C10G45/02, C10G45/32, C10G45/44, C10G45/58 or C10G47/00
- C10G49/10—Treatment of hydrocarbon oils, in the presence of hydrogen or hydrogen-generating compounds, not provided for in a single one of groups C10G45/02, C10G45/32, C10G45/44, C10G45/58 or C10G47/00 with moving solid particles
- C10G49/16—Treatment of hydrocarbon oils, in the presence of hydrogen or hydrogen-generating compounds, not provided for in a single one of groups C10G45/02, C10G45/32, C10G45/44, C10G45/58 or C10G47/00 with moving solid particles according to the "fluidised-bed" technique
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J2208/00—Processes carried out in the presence of solid particles; Reactors therefor
- B01J2208/00008—Controlling the process
- B01J2208/00548—Flow
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- Chemical & Material Sciences (AREA)
- Engineering & Computer Science (AREA)
- Organic Chemistry (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Combustion & Propulsion (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- General Chemical & Material Sciences (AREA)
- Devices And Processes Conducted In The Presence Of Fluids And Solid Particles (AREA)
- Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
Abstract
A kind of fluidized bed reactor of the present invention, including vertical reactor shell, reactor shell internal upper part sets three phase separator, three phase separator includes two different concentric drums of internal diameter, that is inner cylinder and outer barrel, inner cylinder upper end seal cover board is connected by aspiration with reactor head gas vent, and the tube wall setting through-hole of aspiration, it is external that inner cylinder upper portion side wall setting liquid phase material is exported to reactor enclosure.The present invention is on the basis of existing technology, further make full use of fluidized bed reactor upper space, it is preliminary to realize feed separation function, while the utilization rate (improving catalyst in reactor reserve) of reactor can be further improved, it can further promote hydrogenation reaction effect.
Description
Technical field
The invention belongs to boiling bed hydrogenation technical fields, and in particular to a kind of fluidized bed reactor.
Background technology
Boiling bed hydrogenation reaction refers to feedstock oil (predominantly liquid phase), hydrogen (gas phase) carries out adding hydrogen on catalyst (solid phase)
The process of reaction, hydrogenation reaction mainly occur hydrodesulfurization, hydrodenitrogeneration, hydrogenation deoxidation plus hydrogen saturation, are hydrocracked.Instead
Device is answered to be operated under the fluidized state of gas, liquid, solid three-phase, catalyst is in the feedstock oil and hydrogen entered from reactor bottom
Under drive, in fluidized state, entirely different fluid state is in fixed bed reactors.Boiling bed hydrogenation reaction can be with
The inferior feedstock oil of processing high metal, high asphalt content, reaction is with pressure drop is small, temperature is uniform, can add to arrange online and urge
The features such as agent is to keep catalyst activity.
The material discharge mode of existing fluidized bed reactor generally comprises two kinds, and one kind is gas-liquid mixture from reactor top
Portion's mixing discharge；One kind is that gas phase is discharged from reactor head, and liquid phase outlet of the liquid phase from top less than top is discharged.The
A kind of mode is relatively simple, but is needed after material discharge using the further gas-liquid separation of high pressure separation equipment, second way reality
Be to be used using reactor upper space as gas-liquid separation equipment on border, but be only the phase separation of simple gas-liquid, without material into
One step separation function.
Presently, there are two kinds of major type of boiling hydrogen addition technologies, one kind is such as USRe25 by the way of oil phase cycle,
Ebullated bed described in 770, the deficiency of this ebullated bed in practical applications are：To keep solid-liquor separation effect, in reactor
Catalyst amount cannot be too many, and reactor utilization rate is low, fluidized bed reactor utilization rate generally only 40% or so (utilization rate
Refer generally to the percentage that loaded catalyst accounts for reactor volume (disregarding end socket space), fixed bed reactors utilization rate is general
More than 90%)；Reactor has larger space, makes that residence time of the liquid material under no catalytic condition is long, this position does not have
There is hydrogenation reaction, material easily reacts coking at high temperature.Another kind of is that three phase separator is set in fluidized bed reactor,
Gas-liquid-solid separation is carried out in fluidized bed reactor internal upper part, such as the fluidized bed reactor that CN02109404.7 is introduced, by the party
Case can improve the dosage of catalyst, that is, that improves reactor utilizes space, but in reality by three phase separator built in setting
Border in use, catalyst amount improve it is limited --- if catalyst amount increases, under the separating effect of three phase separator is quick
Drop actually improves limited than first kind fluidized bed reactor utilization rate；CN200710012680.9 carries out above-mentioned technology
It is further improved, guide frame is set in three phase separator lower part, using guide frame, increases the operation bullet of three phase separator
Property, it is ensured that three phase separator efficiently separates, and reduces the drag-out of catalyst, improves catalyst inventory, improves reactor and utilizes
Rate, but when in use, still need to the certain area's setting catalyst lean phase region in three phase separator lower part (the region catalytic amount is seldom,
Substantially hydrogenation reaction does not occur), otherwise the separating effect of three phase separator cannot still be met the requirements, and the presence of dilute-phase zone, shadow
The further promotion of reactor utilization rate is rung, also influences hydrogenation reaction effect, and after the amplification of reactor scale, catalyst dress
Amount is more difficult to improve, it is difficult to reach ideal effect.
Therefore, the utilization ratio of fluidized bed reactor how is improved, improves reaction effect, is that the skill solved is badly in need of in this field
Art problem.
Invention content
According to the above-mentioned deficiencies in the prior art, the present invention provides a kind of fluidized bed reactor, reactor is further improved
Utilization rate (improve catalyst in reactor reserve), promote hydrogenation reaction effect, and make full use of on fluidized bed reactor
Portion space, tentatively realizes feed separation.
A kind of fluidized bed reactor of the present invention including vertical reactor shell, is equipped at the top of reactor shell
Gas vent and catalyst inlet, bottom are equipped with material inlet and catalyst outlet, and lower part sets distribution in reactor enclosure body
Disk, reactor shell internal upper part setting three phase separator, there are gaps with reactor shell top for three phase separator, form gas
Phase space, clearance distance be reactor shell 0~20%, preferably 5%~10%；The three phase separator includes interior
Two different concentric drums of diameter：Inner cylinder and outer barrel, the upper and lower ends of the outer barrel are all open, the inner cylinder upper end
Equipped with seal cover board, inner cylinder lower ending opening, for the upper end opening of outer barrel less than seal cover board, the lower ending opening of outer barrel is less than inner cylinder
Lower ending opening；Outer barrel top is direct tube section, and lower part is a taper type contraction section, and the lower ending opening of taper type contraction section is i.e. outer
The lower ending opening of cylinder；Gap is set between the lower ending opening of inner cylinder and the lower ending opening of outer barrel, in order to which material passes through；It is described
Seal cover board connected by aspiration with the gas vent at the top of reactor shell, the setting of the tube wall of aspiration is several
Through-hole, inner cylinder side wall upper part setting liquid outlet are external to reactor enclosure.
The internal diameter of the aspiration is not more than the 150% of reactor shell top gas outlet diameter, not less than anti-
Answer the 50% of device case top diameter gas outlets；The gross area of aspiration tube wall through-hole is not more than the circulation of aspiration
The 150% of cross-sectional area, not less than the 50% of aspiration cross-sectional flow area.
The reactor shell is externally provided with circulating pump, and liquid outlet is connected with circulating pump, circulating pump and and material inlet
Connection, material inlet is recycled to subsequently into reactor enclosure body by the liquid material of discharge.
Bottom setting eddy flow guide plate inside the inner cylinder, generates cyclonic action by the liquid for entering inner cylinder, prevents liquid
Body is taken out of by gas.
The 50%~90% of a diameter of reactor shell internal diameter of the outer barrel top direct tube section；The height of direct tube section is
0.4~3m；Annular space distance between inner cylinder and outer barrel is the 30%~70% of outer barrel corresponding position radius；Inner cylinder upper end with it is outer
The difference in height of cylinder upper end is the 10%~50% of outer barrel radius；Gap between the lower ending opening of inner cylinder and outer barrel contraction section is
The 5%~40% of outer barrel direct tube section radius；The 10% of a diameter of outer barrel direct tube section diameter of outer barrel contraction section lower ending opening~
50%；The angle of throat (acute angle of direct tube section and taper type contraction section) of outer barrel lower part taper type contraction section is 20 °~80 °.
The 75%~85% of a diameter of reactor shell internal diameter of the outer barrel top direct tube section；The height of direct tube section is
0.5~1m；Annular space distance between inner cylinder and outer barrel is the 40%~60% of outer barrel corresponding position radius；Inner cylinder upper end with it is outer
The difference in height of cylinder upper end is the 20%~40% of outer barrel radius；Gap between the lower ending opening of inner cylinder and outer barrel contraction section is
The 10%~30% of outer barrel direct tube section radius；The 15% of a diameter of outer barrel direct tube section diameter of outer barrel contraction section lower ending opening~
35%；The angle of throat (acute angle of direct tube section and taper type contraction section) of outer barrel lower part taper type contraction section is 30 °~60 °.
The outer barrel shrinks pars infrasegmentalis setting direct tube section, i.e. outer barrel is followed successively by direct tube section-contraction section-straight tube from top to bottom
Segment structure.
The lower section setting baffle of the outer barrel lower ending opening, baffle is in spindle small in ends, broad in the middle up and down,
Prevent the fluid in reactor enclosure body from entering three phase separator from outer barrel lower ending opening, baffle axial cross section maximum is straight
Diameter is 1~3 times of outer barrel lower ending opening diameter, is set between baffle and three phase separator outer barrel lower port suitable for gap.
The present invention can be arranged as required to system for detecting temperature, pressure detecting system, fluid flow state detecting system, catalysis
Agent distribution detecting system, material reallocation system, catalyst add heat-extraction system etc. online.
Reaction raw materials can be with heavy, inferior raw material, such as decompression residuum, coal tar, liquefied coal coil, asphalt oil sand, shale oil
Deng.Catalyst is generally solid particle, and particle diameter is generally 0.6~2mm (in terms of isometric spherical shape), catalyst generally with
Aluminium oxide is carrier, at least one such as Mo, W, Ni, Co for active component, while can add related auxiliaries.Catalyst exists
Reactor interior loading amount (in terms of stationary state) is the 50%~85%, preferably 65%~80% of reactor volume, most preferably
72%~78%.Reaction condition can require to determine according to feedstock property and reaction depth, General reactions pressure for 5~
25MPa, reaction temperature are 200~500 DEG C, and hydrogen and feedstock oil standard state lower volume ratio are 300~2000, feedstock oil with
The volume space velocity that catalyst volume (stationary state) is compared is 0.1~2h-1。
For the present invention by structures such as three phase separator, aspirations, gas phase of the gaseous phase materials at the top of reactor shell is empty
Between enter aspiration when, actual internal area is substantially reduced, and flow velocity significantly increases so that the pressure drop of three phase separator inner cylinder
It is low, promote the weight component separation of liquid phase in inner cylinder, light component more discharged into reactor from gas phase, and heavy constituent from
Liquid-phase outlet discharge Posterior circle returns reactor and carries out circular response, enhances reaction, improves the conversion level of heavy constituent.Match
Closing eddy flow guide plate has more prominent effect, and cyclonic action causes the pressure of inner cylinder central area further to reduce, is more advantageous to
The separation of light component.Aspiration can also carry a part of liquid phase material discharge reactor secretly, this does not influence the object of the invention reality
It is existing, and reaction environment in reactor can be optimized, the mode of operation that liquid phase discharge material all recycles may be used at this time,
Avoid the build-up effect that reaction environment deteriorates in the reactor that all cycle generates.
In addition, it is not only in that three-phase separate by largely furtheing investigate the factor for showing to influence three phase separator separating effect
Structure, material system status from device, also have much relations with earth rotation.Gas, liquid, solid three-phase state in reactor enclosure body,
For gas, liquid generally in the state that flows up, solid catalyst is in boiling quick condition.Earth rotation is to above-mentioned material shape
State has certain active force, forms slight cyclonic action, in the larger reactor of industry, due to larger, and this rotation
Stream effect more shows.As a result, catalyst is more assembled in the region close to reactor wall, reactor radial center area
Domain is more sparse.This effect produces the separating effect of existing three phase separator and significantly affects, that is, works as loaded catalyst
During increase, the solid catalyst that three phase separator is separated settles back the resistance increase in reactor, is taken out of by liquid material
The chance of reactor improves, and reactor is made to take catalytic amount increase out of.To solve the problems, such as this, usually under three phase separator
Portion set catalyst dilute-phase zone, with overcome catalyst sedimentation flow back resistance, but the measure the result is that reactor utilization rate
It reduces, reaction effect is affected.Before making the present invention, those skilled in the art do not recognize influence ebullating bed reactor
The full content of three phase separator separating effect influence factor in device, into without proposing suitable solution.
The present invention is on the basis of the studies above, for earth rotation to the shadow of flow state in large-scale fluidized bed reactor
It rings, has redesigned novel ebullated bed three phase separator, solved problem of the prior art, obtained following technique effect：
1st, the solid catalyst that three phase separator separates is flowed back into reaction in reactor radial center regional subsidence
In device, when solving high catalyst loadings, the big problem of resistance of catalyst sedimentation reflux ensure that three phase separator in height
Still there is good separating effect during loaded catalyst.
2nd, the catalyst of loaded catalyst ratio, particularly large-scale industry fluidized bed reactor can be further improved
Filling ratio.While reactor volume utilization rate is improved, catalyst lean phase region is reduced or eliminated, improves plus hydrogen is anti-
Answer effect.
3rd, reaction effect problem is influenced caused by catalyst distribution unevenness caused by overcoming earth rotation.The prior art
In, not considering the eddy flow of earth rotation influences, and catalyst is unevenly distributed to a certain extent, and existing three phase separator will divide
From the catalyst sedimentation got off to reactor wall region, exacerbate it is this be unevenly distributed, influencing three phase separator separation effect
While fruit, reaction effect is also influenced.The method of the present invention solves the deficiency.
4th, when gas-phase space of the gaseous phase materials at the top of reactor shell enters aspiration, actual internal area contracts significantly
Small, flow velocity significantly increases so that the pressure reduction of three phase separator inner cylinder promotes the weight component separation of liquid phase in inner cylinder, more
Light component mostly is discharged into reactor from gas phase, and heavy constituent is returned reactor from liquid-phase outlet discharge Posterior circle and is recycled
Reaction, enhances reaction, improves the conversion level of heavy constituent.Coordinate eddy flow guide plate that there is more prominent effect, cyclonic action
So that the pressure of inner cylinder central area further reduces, it is more advantageous to the separation of light component.
Description of the drawings
Fig. 1 is the structure diagram of the present invention.
Wherein：1st, material inlet；2nd, distribution plate；3rd, reactor shell；4th, baffle；5th, outer barrel；6th, inner cylinder；7th, it seals
Cover board；8th, catalyst inlet；9th, gas vent；10th, liquid outlet；11st, catalyst outlet；12nd, prime feed system；13、
Eddy flow guide plate；14th, circulating pump；15th, aspiration.
Specific embodiment
With reference to embodiment, the present invention will be further described, but is not construed as limiting the invention.
Embodiment 1
The internal diameter 200mm of reactor shell 3, the height 3500mm of reactor shell 3, three phase separator height 400mm,
The diameter 300mm of the 5 top direct tube section of outer barrel of three phase separator, the annular space distance between inner cylinder 6 and outer barrel 5 is 80mm, inner cylinder
The difference in height of 6 upper ends and 5 upper end of outer barrel is 60mm, and the gap between the lower ending opening of inner cylinder 6 and the contraction section of outer barrel 5 is
60mm, 6 upper end of inner cylinder adds seal cover board 7, and aspiration 15 is set to be connected with reactor head gaseous phase outlet, aspiration
The 15 a diameter of and outer same diameters of row pipeline (50mm) of reactor gas phase, the gross area of 15 tube wall through-hole of aspiration, which is equal to, to be aspirated
15 cross-sectional area of pipeline.The a diameter of 90mm of contraction section lower ending opening of outer barrel 5, the angle of throat of 5 lower part taper type contraction section of outer barrel
35 ° of (acute angle of direct tube section and taper type contraction section).4 spindle axial cross section maximum of baffle is a diameter of
150mm.Cold model experiment is carried out, using kerosene as liquid, oil inlet quantity is 60~120L/hr；Gas phase selects nitrogen, air inflow 3
~4Nm3/hr.Solid phase select grain size be 0.7~0.8mm aluminum oxide micro-sphere catalyst, catalyst inventory (by it is static when in terms of)
55%~80% for reactor dischargeable capacity (disregarding end socket space).It the results are shown in Table 1.
1 cold model experiment result of table
From cold model experiment as can be seen that a kind of fluidized bed reactor of the present invention has good solid separation effect
Fruit, applicable operating range are wider.
Embodiment 2
2 structure of embodiment is as shown in Figure 1, compared with Example 1, the lower part setting eddy flow guide plate 13 in three phase separator,
Liquid phase uses dead oil (170~320 DEG C of boiling range), is tested under the conditions of 0.2MPa (gauge pressure) and 200 DEG C, into
Oil mass 80L/hr, air inflow 3Nm3/ hr, catalyst inventory 65V%, it is other same as Example 1, it the results are shown in Table 2.
Comparative example
Compared with Example 2,6 upper end opening of inner cylinder is not provided with aspiration 15, is not provided with eddy flow guide plate 13, Qi Tayu
Embodiment 2 is identical, the results are shown in Table 2.
2 comparison of test results of table
From test data as can be seen that the method for the present invention can extract more liquid products out from gas phase, and extract out
Liquid product light component it is more.
Claims (8)
1. including vertical reactor shell (3), gas vent is equipped at the top of reactor shell (3) for a kind of fluidized bed reactor
(9) and catalyst inlet (8), bottom is equipped with material inlet (1) and catalyst outlet (11), material inlet (1) and prime into
Material system (12) is connected, the interior lower part setting distribution plate (2) of reactor shell (3), reactor shell (3) internal upper part setting three-phase separate
From device, it is characterised in that：There are gaps with reactor shell (3) top for three phase separator, form gas-phase space, clearance distance is
The 0~20% of reactor shell (3)；The three phase separator includes two different concentric drums of internal diameter：Inner cylinder (6) and outer
Cylinder (5), the upper and lower ends of the outer barrel (5) are all open, and the inner cylinder (6) upper end is equipped with seal cover board (7), inner cylinder
(6) lower ending opening, the upper end opening of outer barrel (5) is less than seal cover board (7), and the lower ending opening of outer barrel (5) is less than under inner cylinder (6)
End opening；Outer barrel (5) top be direct tube section, lower part be a taper type contraction section, lower ending opening, that is, outer barrel of taper type contraction section
(5) lower ending opening；Gap is set between the lower ending opening of inner cylinder (6) and the lower ending opening of outer barrel (5)；The seal cover board
(7) it is connected by aspiration (15) with the gas vent (9) at the top of reactor shell (3), the tube wall of aspiration (15) is set
Put several through-holes, inner cylinder (6) side wall upper part setting liquid outlet (10) to reactor shell (3) outside.
2. a kind of fluidized bed reactor according to claim 1, it is characterised in that：The internal diameter of the aspiration (15)
No more than the 150% of reactor shell (3) top gas outlet (9) diameter, exported not less than reactor shell (3) top gas
(9) the 50% of diameter；The gross area of aspiration (15) tube wall through-hole is no more than the cross-sectional flow area of aspiration (15)
150%, not less than the 50% of aspiration (15) cross-sectional flow area.
3. a kind of fluidized bed reactor according to claim 1, it is characterised in that：Described reactor shell (3) peripheral hardware
There is circulating pump (14), liquid outlet (10) is connected with circulating pump (14), circulating pump (14) and is connected with material inlet (1).
4. a kind of fluidized bed reactor according to claim 1, it is characterised in that：The internal bottom of the inner cylinder (6)
Eddy flow guide plate (13) is set.
5. a kind of fluidized bed reactor according to claim 1, it is characterised in that：The diameter of outer barrel (5) top direct tube section
50%~90% for reactor shell (3) internal diameter；The height of direct tube section is 0.4~3m；Between inner cylinder (6) and outer barrel (5)
Annular space distance is the 30%~70% of outer barrel (5) corresponding position radius；Inner cylinder (6) upper end and the difference in height of outer barrel (5) upper end are
The 10%~50% of outer barrel (5) radius；Gap between the lower ending opening of inner cylinder (6) and outer barrel (5) contraction section is straight for outer barrel (5)
The 5%~40% of cylinder section radius；The 10%~50% of outer barrel (5) contraction section lower ending opening a diameter of outer barrel (5) direct tube section diameter；
The angle of throat of outer barrel (5) lower part taper type contraction section is 20 °~80 °.
6. a kind of fluidized bed reactor according to claim 1, it is characterised in that：The diameter of outer barrel (5) top direct tube section
75%~85% for reactor shell (3) internal diameter；The height of direct tube section is 0.5~1m；Between inner cylinder (6) and outer barrel (5)
Annular space distance is the 40%~60% of outer barrel (5) corresponding position radius；Inner cylinder (6) upper end and the difference in height of outer barrel (5) upper end are
The 20%~40% of outer barrel (5) radius；Gap between the lower ending opening of inner cylinder (6) and outer barrel (5) contraction section is straight for outer barrel (5)
The 10%~30% of cylinder section radius；The 15% of outer barrel (5) contraction section lower ending opening a diameter of outer barrel (5) direct tube section diameter~
35%；The angle of throat of outer barrel (5) lower part taper type contraction section is 30 °~60 °.
7. a kind of fluidized bed reactor according to claim 1, it is characterised in that：It is straight that outer barrel (5) shrinks pars infrasegmentalis setting
Cylinder section.
8. a kind of fluidized bed reactor according to claim 1, it is characterised in that：It is set below outer barrel (5) lower ending opening
Put baffle (4), for baffle (4) in spindle small in ends, broad in the middle up and down, baffle (4) axial cross section maximum is straight
Diameter is 1~3 times of outer barrel (5) lower ending opening diameter.
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| CN109967002A (en) * | 2019-04-26 | 2019-07-05 | 河南百优福生物能源有限公司 | The three phase separator of biomass pyrolysis liquid fluidized bed reactor and its application |
| CN109999729A (en) * | 2019-04-26 | 2019-07-12 | 上海华畅环保设备发展有限公司 | Boiling bed hydrogenation catalyst reactor online eddy flow method for activation recovering in situ and device |
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| CN108144555B (en) | 2024-04-12 |
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